Note: Descriptions are shown in the official language in which they were submitted.
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PROCESS FOR REMOVING NOX FROM NITROSYLSULPHURIC ACID
Description
This invention relates to a process of removing NOX from ni-
trosyl hydrogensulfate by mixing nitrosyl hydrogensulfate in
a mixing reactor with sulfuric acid, which is saturated with
S02r where a sulfuric acid containing N203 is withdrawn from
the mixing reactor, and a stripping gas is passed through the
withdrawn sulfuric acid.
Such process is known from GB-A-0,348,866. For the expulsion
of residual nitrogen oxides from the sulfuric acid flue gas
or an inert gas is passed through the sulfuric acid, with the
temperature lying in the range from 100 to 200 C. In Database
WPI, AN91-108 779 it is described that NOX-containing sulfu-
ric acid (spent acid) is mixed with circulating acid and
added to a so-called second column. In the lower portion of
the second column S02 gas is introduced, which comes from a
so-called first column. Part of the circulating acid with-
drawn from the second column is added to the first column, to
which a surplus of S02 is supplied. The exhaust gas of the
second column contains no S02, and the sulfuric acid with-
drawn from the first column, which is free from NOX, contains
75 wt-% H2SO4. Mixing the spent acid with sulfuric acid satu-
rated with S02 does not take place in the known process.
The object underlying the invention is to remove NOX from ni-
trosyl hydrogensulfate in a simple and inexpensive way. In
accordance with the invention this is accomplished in the
above-stated process in that the N203-containing sulfuric
acid withdrawn from the mixing reactor is added to a satura-
tion reactor, where in the lower portion of the saturation
AMENDED SHEET
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reactor an S02-containing gas is introduced at the same time,
which at least in part flows upwards through the N203-con-
taining sulfuric acid, that water is introduced into the
saturation reactor, and from the saturation reactor a virtu-
ally NOX-free sulfuric acid saturated with S02 is withdrawn,
which has a H2SO4 concentration of 5 to 60 wt-%, and a par-
tial stream of which is passed into the mixing reactor, where
S02 is supplied to the mixing reactor in a stoichiometric
surplus of at least 2 wt-% with reference to the NOX content
of nitrosyl hydrogensulfate.
In accordance with the invention, the term NOX refers to a
mixture of NO and N02. NOX is present in sulfuric acid as
dissolved nitrosyl hydrogensulfate. Nitrosyl hydrogensulfate
is formed from NO, which is contained in S02-containing gas.
The S02-containing gas originates for instance from a roast-
ing, sulfur combustion, sulfate separation or metallurgical
process. NO is oxidized at the oxidation catalyst of a sulfu-
ric acid plant for up to 50 % to form N02. The mixture of NO
and N02 is reacted with sulfuric acid to form nitrosyl hydro-
gensulfate as follows:
NO + N02 + 2H2SO4 --> 2HNOSO4 + H20
It is known that S02 reacts with nitrosyl hydrogensulfate by
forming sulfuric acid and nitrogen oxides:
S02 + 2HNOSO4 + 2H20 --> 3H2SO4 + 2N0
In the production of sulfuric acid nitrosyl hydrogensulfate,
usually with a NOX content of more than 2.5 wt-%, is sepa-
rated as a condensate. The NOx content is present in the con-
densate as nitrosyl hydrogensulfate in addition to sulfuric
acid.
AMENDED SHEET
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In formal terms, nitrosyl hydrogensulfate can be reacted with
S02 and water to form sulfuric acid and N2. The redox reac-
tion takes place between the dissolved S02 in the form of
S032 with the N203 in the form of N02 , which was produced in
the hydrolysis of nitrosyl hydrogensulfate. The reduction of
the nitrogen oxides NO and N02 to nitrogen is effected in the
AMENDED SHEET
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hydrolysis of nitrosyl hydrogensulfate with dilute, S02-satu-
rated sulfuric acid in that in the diluting solution the re-
ducing agent is provided in the form of S032 in an overstoi-
chiometric amount, so that the equilibrium is shifted towards
the formation of N2.
It is an advantage of the present invention that the amount
sulfuric acid present in a condensate containing nitrosyl hy-
drogensulfate can be recirculated to a sulfuric acid produc-
tion without any NOX. In accordance with the conventional
processes the condensate is withdrawn from the process and
must be subjected to a treatment or be disposed of. A par-
ticular advantage of the inventive process consists in that
nitrogen is formed from the noxious substance NOX and is dis-
charged together with the exhaust gas.
Preferably, S02 is supplied to the mixing reactor in a stoi-
chiometric surplus of at least 5 wt-% with reference to the
NOX content of nitrosyl hydrogensulfate. With this surplus of
S02 a good result is achieved in the reduction of the NOX
content. S02 is not lost as a result of the reduction of NOX
to N2, but is oxidized to form SO42 . Excess S02 can be sup-
plied to a plant for the production of sulfuric acid, so that
an extensive treatment is not necessary.
Advantageously, the sulfuric acid concentration after the ad-
dition of SOZ is 5 to 30 wt-%. In this range of the sulfuric
acid concentration particularly good results are achieved for
the reduction of NOX to N2.
In accordance with an advantageous aspect of the invention
gaseous S02 is brought into aqueous solution in a saturation
reactor designed as packed column, and is combined with the
NOX-containing sulfuric acid as an aqueous solution. The S02
saturation is promoted by operating the saturator under an
increased gas pressure.
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In accordance with the invention, the NOX content of a NOX-
containing sulfuric acid (nitrosyl hydrogensulfate) or a NOX-
containing sulfuric acid mixture is reduced. The process in
accordance with the invention can advantageously not only be
applied to NOX-containing sulfuric acid, but with very good
results also to mixtures containing NOX and sulfuric acid,
such as nitrating acid or sulfuric acid contaminated with
other compounds.
Embodiments of the invention will be explained in detail with
reference to the drawing and examples. The drawing represents
a flow diagram of the process.
The most important parts of the process are the reactor (X)
for the saturation of S02 and the mixing reactor (Y) for hy-
drolysis and redox reaction of nitrosyl hydrogensulfate with
S02-containing dilute sulfuric acid. S02-containing roaster
gas is introduced via line (1), and water is introduced via
line (4) into the lower portion of the saturation reactor
(X). Via line (3) nitrosyl hydrogensulfate or condensate con-
taining said acid is supplied to the mixing reactor (Y). In
principle, dilute sulfuric acid is circulated between the re-
actors (X) and (Y) via lines (5), (6), (6A), (7) and (8).
Sulfuric acid formed is withdrawn via line (6B), and N2 is
discharged together with the exhaust gas via line (2).
Via line (5), sulfuric acid is withdrawn from the saturation
reactor (X) and passed through a pump (9). Said sulfuric acid
is saturated with S02, is virtually NOX-free, and has a H2SO4
concentration of 5 to 60 wt-% and mostly not more than 35 wt-
%. From the pump (9), the sulfuric acid is withdrawn via line
(6). A partial stream of the acid is supplied to the mixing
reactor (Y) via line (6A). The acid withdrawn from the reac-
tor (Y) via line (7), which still contains N203, is supplied
to the indirect cooler (W). Via line (10), the cooler is sup-
plied with cooling water, which is withdrawn via line (11).
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Cooled sulfuric acid is introduced into the saturation reac-
tor (X) via line (8). The reactor (X) contains at least one
packed bed. In the reactor (X) upwardly flowing S02-contain-
ing gas serves as stripping gas for removing residual nitro-
gen oxides from the sulfuric acid supplied via line (8).
Example 1:
In an arrangement as shown in the drawing the procedure is as
follows:
Via line (3), 240 kg/h condensate with a nitrosyl hydrogen-
sulfate content of 9.5 % HNOSO4 corresponding to 6.8 kg/h
N203 are introduced into the mixing reactor (Y). The conden-
sate comes from a sulfuric acid production. Via line (6A) an
S02-saturated sulfuric acid with 20 wt-% H2SO4 is supplied to
the reactor (Y), the condensate and S02-saturated sulfuric
acid are mixed. The dissolved S02 reacts with nitrosyl hydro-
gensulfate to form sulfuric acid and nitrogen. The mixture is
withdrawn via line (7), and behind the block cooler (W) still
has a content of 465 mg N203/1, which corresponds to a con-
tent of 2.0 kg N203/h. In the saturation reactor (X) the cir-
culating sulfuric acid is saturated with S02, where S02-con-
taining roaster gas, which contains 0.28 g/h NOX, is supplied
via line (1). The concentration of sulfuric acid is adjusted
to 20 wt-% H2SO4 by means of a controlled addition of water
through line (4). The roaster gas leaving the reactor (X) via
line (2) has a reduced S02 content and is returned to the
sulfuric acid production as a wet gas. The gas in line (2)
contains 3.125 mg NOX/Nm3 corresponding to 2.0 kg N203 per
hour. In the sulfuric acid in lines (6B) and (6A) NOx could
no longer be detected. The denitrating conversion was 71.75
s
o.
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Example 2:
Example 2 is carried out like Example 1, but with the follow-
ing differences:
S02-saturated sulfuric acid containing 16 wt-% H2SO4 is sup-
plied to the mixing reactor (Y) via line (6A). Behind the
block cooler (W) the sulfuric acid in line (8) contains 400
mg N203/1 corresponding to 1.7 kg N203/h. After a controlled
addition of water through line (4), a sulfuric acid with a
concentration of 16 wt-% H2SO4 is produced in the saturation
reactor (X) and withdrawn via line (5). This sulfuric acid is
NOX-free. The denitrating conversion was 80.23 %.
Example 3:
The procedure is as in Examples 1 and 2, but with the follow-
ing differences:
Via line (3) 190 kg/h condensate are introduced into the mix-
ing reactor (Y). The condensate has a nitrosyl hydrogensul-
fate content of 7.5 wt-% HNOSO4 corresponding to 4.3 kg N203
per hour. The condensate is mixed in the mixing reactor (Y)
with a 33 %, S02-saturated sulfuric acid from line (6A). Be-
hind the block cooler (W), the sulfuric acid in line (8) con-
tains 350 mg N203/1 corresponding to 1.5 kg N203/h. In the
saturation reactor (X) a sulfuric acid with a concentration
of 33 wt-% H2SO4 is adjusted through a controlled addition of
water and withdrawn through line (5). The acid is NOX-free.
The SO2 gas withdrawn via line (2) contains 4700 mg NOX/Nm3
corresponding to 3.0 kg N203/h. The denitrating conversion is
34.5%.
The comparison of Examples 1, 2 and 3 clearly illustrates
that there is a dependence between the NOX conversion and the
concentration of the circulating sulfuric acid. The higher
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the concentration of the circulating sulfuric acid, the lower
the denitrating conversion.
The advantage of a rather high denitrating conversion con-
sists in the fact that the circulating amount of NOX is
lower. NOX which is not discharged from the denitrating plant
gets back to the main gas stream of the sulfuric acid plant,
where nitrosyl hydrogensulfate is formed again. A lower deni-
trating conversion requires a larger denitrating plant.
